BR0107842B1 - fluid processing system. - Google Patents

Abstract

A column apparatus containing a shallow bed of material between fluid transporting fractals of large active surface area results in highly efficient processing with small equipment size.

Description

Report of the Invention Patent for "FLUID PROCESSING SYSTEM".

TECHNICAL FIELD

Many fluid processes operate by passing fluids through material beds. These processes include chromatography, ion exchange, adsorption, catalytic reaction, etc. This invention is directed to such problems in general.

PREVIOUS TECHNIQUE

Fluid processes characteristically have severe limitations on operation due to loss of bed pressure, kinetics and flow uniformity. These limits are imposed, for example, on productivity, process efficiency, energy use, system size, environmental compatibility and capital / operating costs.

As an example of how these limits occur, the flow through a bed may be restricted because as the flow increases, the pressure of the bed increases. Pressure loss can reach a point where the pressure rating of a column containing the bed may be exceeded, the bed may begin to unacceptably compress, the bed particles may be destroyed and excessive energy may be required. for an operation. Clearly, this effect imposes limits on productivity (flow limits) and cell design and costs (higher pressure requires additional structural strength).

As another example, high linear velocities can result in an unacceptably bad interaction or reaction of a fluid with the bed material. That is, the system's kinetic demands are self-limiting. Excessively high linear velocity of a fluid through a bed will result in insufficient fluid contact time with the bed particles. Clearly, this imposes limits on productivity.

(Again, flow is limited.)

Spreading a bed over a wide (large cross section), shallow (shallow depth or short path) geometry rather than a high (long stroke path) and narrow (relatively small cross section to flow direction) geometry will reduce the loss. bed and the linear velocity of a fluid passing through the bed.

While both of these effects are very beneficial, such a decoloured construction does not prevail because of the difficulty of ecoletically distributing fluid across a wide, hollow bed (a large cross section). Any inhomogeneity or turbulence in the fluid introduced into the column normally cannot be attenuated through a wide and shallow bed, so that the inhomogeneities are reflected as inefficiency and unacceptable processing. For example, in chromatography, these problems result in bandwidth and poor separation of components from a feed mixture.

A representative device is shown in Brown U.S. Patent No. 4,673,507. The '507 patent shows a fluid treatment apparatus which can be used for a shallow bed operation. However, this device lacks significantly distributed fluid supply and collection systems, and is dependent on maintaining the bed in an overpressed condition. Substantially uniform fluid flow distribution across the bed is achieved by employing (substantially uniform) fine particle size resins, which are maintained in an overpressure condition. Here, the term 'overpressed' is used to mean that the particles are confined to the resin bed so that they are subjected to compression at all times.

This device inherently restricts the flow of process fluid through the bed.

U.S. Patent No. 5,626,750 to Chinn shows an apparatus for treating fluid. In this apparatus, the first and second "particle cavities" are provided above and below the retained particle bed. Uniform fluid flow through the bed is simply provided by pressure loss through the bed. Pressure loss across the bed is a function of pressures in the first and second cavities. No provision is made to substantially control fluid flow characteristics (vortices or turbulent zones) in the flow-through fluid flows near the bed surface.

It would be an advance to provide a fluid processing apparatus which has reduced pressure loss through a media bed and also has reduced fluid flow (velocity) at increased volumetric flow through the bed. A preferred apparatus would provide control by the process fluid flow to reduce mixing and turbulence near the bed to resist inhomogeneities in the processing flow.

DESCRIPTION OF THE INVENTION

The present invention provides an apparatus for a fluid processing system, which involves passing a fluid through a processing tube configured to have a diameter substantially greater than its height (the distance between its inlet end and its outlet end). . The invention is operable in systems in which the ratio of diameter (D) to height (h) of the processing bed is as high as 20: 1 or more. The invention is advantageously applied to beds with D: h ratios approaching 2: 1, but D: h ratios beyond about 3: 1 are presently preferred. The term "processing bed" refers to any confined mass of conventional or special purpose processing material (medium) contained by a cell or column through which fluids are passed. Typical materials for such processing include inorganic or organic lining materials, chromatography media, ion exchange media, absorption or adsorption media, enzymatic and cationic reagents.

A fluid dispenser typically is arranged for introducing process fluid into the inlet end of the bed with a density of at least 18.58 dispensing outputs per square meter (200 dispensing outputs per square foot). ). A fluid collector typically is arranged to collect the processed fluid once at the resin bed outlet end. Generally, it is preferred that the manifold be arranged to fluidly flow through collection inlets with a density of at least 18.58 per square meter (200 per square foot). It is contemplated to provide inlets and / or outlets with a density of 310,000 per square meter (200 per square inch) or more. At present, it is preferred to construct the manifold and collector from recursively arranged fractal elements. Systems in accordance with the principles of the present invention may be constructed to produce processing flow conditions with a pressure loss across the bed of 34.47 kPa (5 psi) media.

A system according to the present invention may further include a second processing bed with an inlet side, an outlet ladder and a diameter equal to at least twice the distance between the inlet end and the outlet side. A second fluid dispenser may be arranged to introduce the processed fluid once into the inlet side of the second bed. The second manifold also desirably has a density of at least 2,153 manifold outlets per square meter for the promotion of one-dimensional flow with minimized mixing and turbulence in the process fluid. A second fluid collector is then disposed generally for collecting the processed fluid twice on the outlet side of the second resin bed. Currently, it is preferred that the first and second fluid distributors are formed from the same fractal structure. It is also preferred that the first and second fluid collectors are formed from the same fractal structure, and are similar to the dispensers. A desirable recursive fractal element can be characterized as having a formato "shape. Other factual elements, including those with three-dimensional shapes, are also contemplated for use in manifold or manifold structures.

BRIEF DESCRIPTION OF DRAWINGS

In the drawings which illustrate what is currently considered to be the best mode for carrying out the invention and in which like reference numerals refer to like parts in different views or embodiments:

Figure 1 is a cross-sectional plan view of a typical embodiment of this invention, Figure 2 is a detail of an edge portion indicated by baffles 2-2 in Figure 1;

Figure 3 is a cross-sectional plan view of an alternative embodiment of this invention having an empty space left between the bed and the top distributor;

Figure 4 is a plan view of one embodiment having supports for end distributors;

Figure 5 is a top view of a typical detopic end plate;

Figure 6 is a top view of a representative fractal distributor embodiment; and

Figure 7 is a top view of an alternative embodiment, similar to the fractal distributor of Figure 6, but with an additional fractal iteration partially illustrated at the outer periphery.

BEST MODE FOR CARRYING OUT THE INVENTION

Figure 1 illustrates a typical fluid treatment apparatus according to this invention, generally indicated at 102. The apparatus typically includes a top plate 106, a bottom plate 110, and a sidewall 112. As illustrated, sidewall 112 forms a ring-like structure for enclosing a volume between top and bottom plates 106 and 110. The apparatus will be described with reference to a substantially circular sidewall 112, although such a structural limitation is not required for the practice of this invention. One or more sidewalls 112 may be constructed to form virtually any shape cross section through the apparatus.

Currently, it is preferred to mount top and bottom plates 106 and 110 to the side wall 112 in a fluid tight fit with the top and bottom gaskets 114 and 116, respectively. The joint structure which can be disassembled is generally preferred, as is the bolted joint interface generally indicated at 120 in the form of an attachment 102.

With further reference to Figure 1, the top plate 106 generally carries one or more fluid windows 124 for the passage of process fluids therethrough. The fluid window 124 is desirably constructed in fluid communication with an orifice distribution network disposed in a fractal distributor 128. A distributor 128 preferably functions to distribute the process fluid in a configuration which is suitable for approximates a homogeneous arrangement of entry or exit points in space. The main purpose of such a dispenser is to produce a process fluid flow directed substantially in only one direction. Currently, it is preferred to provide the dispenser 128 as a fractal. A bed 132 formed of a suitable working medium is typically disposed between the fractal distributors 128 and 136.

In operation, under a top-down flow, the manifold 136 functions as a manifold. A distributor 136 is typically similar in structure to distributor 128, but in any case generally provides a homogeneous arrangement of entry or exit points in space. The fluid window 138, in fluid communication with the dispenser 136, functions to pass process fluids through the bottom plate 110. It can now be seen that process fluids introduced into the apparatus 102 through the window 124 can pass through the 132. The process fluid may be distributed and collected in a substantially homogeneous manner by the fractional manifolds 128 and 136 on opposite sides of the bed 132. The manifolds 128 and 136 minimize turbulence and mixing in the process fluid. at zones near the top and bottom surfaces of the bed 132. The process flow may alternatively be directed in the opposite direction, with window 138 acting as an inlet and window 128 as an outlet window. For convenience, the apparatus will generally be described from this point on with a top-down flow condition. In a top-down flow condition, the top manifold 128 functions as a manifold, and the bottom manifold 136 functions as a manifold.

Figure 2 illustrates a detail view of a structure typically included in preferred embodiments of the invention. The illustration of Figure 2 depicts a typical mirror image construction on the inlet and outlet sides of the device. Three zones are indicated by the height of the apparatus, representing a fractal distributor zone 142, a bed spreader zone 144, and a second fractal distributor zone 146. The fractal distributor zone 142 houses the fractal distributor 128, and the distributor zone 146 houses the fractal distributor 136. The distributor zones do not have to fill the entire space between bed 132 and the top or bottom plates 106 and 110, respectively. A space may be maintained, for example, above a bed 132 for fluidization of bed 132.

Fractal distributor zones typically work to minimize mixing and turbulence near bed surfaces. A distributor 128 or 136 desirably provides a deflected outlet population at a fluid / manifold interface to approach a distributed fluid flow having only one velocity component directed toward or away from. a bed surface 132. Bed zon 144 houses bed 132, which has top and bottom surfaces 148 and 150, respectively. The bed zone 144 may be defined by the top and bottom surfaces formed by a web, mesh, membrane or other retaining elements (not shown).

Figure 3 illustrates an alternative embodiment 154 of this invention with a void 156 left between bed 132 and top distributor 128. The invention can operate efficiently in this configuration. Alternative mode 154 permits internal fluidization which is required for common steps such as bed backwashing or continuous fluidized bed operation. The void space 156 allows the bed material 32 to have sufficient space in which to move in a vertical direction for purposes. backwashing or fluidizing the bed 132.

Figure 4 illustrates internal supports 160, which may be used if the shallow cell diameter becomes too large to properly support the end distributors. The brackets 160 preferably intercept the fractal distributors 128 and 136 in white areas to prevent any interference with the flow of process fluid. Flat rods or plates are examples of a support structure which can be used on a support element 160.

Figure 5 illustrates a top end plate 106 with a fluid window 124 located approximately on a central axis. One or more of these windows 124 may be located in non-axial locations. However, at present, it is preferred to have only one of these windows 124 centrally located through the end plate 106. The location of the window 124 may be determined for manufacturing reasons and thus may be decentralized. Generally, it is desired to provide the window 124 in a convenient location for connection to the dispenser 128. A plurality of screw holes 164 may be provided spaced around the perimeter of the illustrated plate 106 for forming the junction structure 120. A bottom end plate 110 It is typically structured similarly or symmetrically to the top plate 106.

Figure 6 illustrates a typical fractal distributor embodiment128 suitable for this apparatus. The embodiment illustrated is only an example of a distributor 128, and represents only a desirable arrangement of distribution structure. A virtually infinite number of variations in the structural configuration of a distributor 128 are possible.

Continuing with reference to Figure 6, the individual conduits forming distributor system 128 are placed in separate planes and do not intersect. Arched sectors 164 and 168 are illustrated in progressive stages of the sport. The fluid introduced in window 124 is divided into the flow through successively divided conduit branches. As illustrated, fluid flowing from window 124 is divided into six conduits 172. Each of conduits 172 may subsequently be divided into three or six conduits 174 (may have the mirror image in planes above and below conduits 172). The conduits 174 are then divided for multi-conduit fluid flow 176. The recursive division process may be continued, as desired, to provide a sufficient density of fluid outlets or inlets. propagate successive divisions of the conduit structure into a recursive progression of fractal elements. Successive duct-splitting at least doubles the number of outlets to the cell, and increasingly spreads outlets in a more even distribution over the volume occupied by a 128 manifold. The outlets are not necessarily oriented to have a full-direction directed opening from a distributor towards a bed. Simply spacing the outlets evenly in a volume occupied by the dispenser 128 promotes one-dimensional flow towards a bed 132, and minimizes turbulence in the process fluid.

The recursive addition of shrinking ducts allows the apparatus to be constructed with progressively shallower cells and progressively shallower internal beds. As an example using a fluid introduction into a cell, as the number of fluid outlets increases, the distribution of these outlet points becomes more homogeneous across a volume. The introduced fluid therefore has turbulence or reduced internal mixture. The resultant effect is that substantially every velocity indicator describing the movement of the process fluid is directed perpendicular to the bed. Ideally, a section of plane through the introduced process fluid, and transverse to the flow direction, would remain flat as the process fluid approached and passed through the bed. As fluid flow becomes more uniform, less attenuation of fluid velocity vector components is required from the bed itself, or from a boundary layer immediately adjacent to the bed surface. Therefore, the bed and the processing cell may have correspondingly reduced thickness, resulting in a "shallower" cell structure.

The term "fractal" as used in this exhibition refers to a device constructed as a distributor or collector (128 or 136), which has inputs or outputs connected through conduits constructed and disposed substantially in accordance with the principles of fractal geometry. Fractal structures are mathematical constructs that have scale invariance. In these structures, a self-similar geometry reappears on many scales. Typical manifolds or manifolds 128 or 136 are desirably shaped into conduits arranged in fractal patterns using any well-known manufacturing technique such as tube dies, molded or machined tiles, or stamped plate. Outlet or inlet hole density can be recursively increased by doubling a basic pattern (fractal) on an increasingly smaller scale.

A simpler fractal is a simple "T" intersection, formed by the intersection of a first right-angled conduit with a second generally smaller-diameter conduit. This simplest case doubles the number of inputs or outputs in a distribution system each successive generation of fractal structure. The outputs of each generation of fractal structures typically are connected to inputs of subsequent weak generation. The outputs of the final generation fractal structure correspond to the distributor 128 outputs.

Of course, other more complicated fractal patterns are possible in the present device. For example, a fractal pattern based on the recursive propagation of a fractal element that approaches an "H" format is illustrated in Figures 6 and 7. Fractals can also be three-dimensional. A three-dimensional fractal element can be characterized as having four rays radiating from a cube, each ray in fluid communication with paired outputs. Such a fractal element can have outputs located at the eight corners of an imaginary cube. A second three-dimensional fractal element can have three rays radiating from a cube. Each radius may terminate at one outlet, or communicate with an additional conduit structure, to form an increased number of outlets. Moreover, the distributor 128 or collector 136 may contain more than one fractal configuration. For example, a generation of "H" shaped fractal structures can feed a subsequent generation of "T" shaped fractal structures, and so on.

Generally, it is preferred that the total cross section of successive generations of fractal structure be substantially the same, or larger than the total cross section of the source generation. Such a cross-sectional arrangement helps minimize fluid velocity in the inlet and outlet ports. In any case, it is desired that all conduit structures in a particular generation be hydraulically similar to promote uniformly distributed flow throughout the generation.

Figure 7 illustrates the same fractal spread as in Figure 6, but with an additional fractal iteration applied to the outer area. These iterations are the key to the progressive retraction of this device height invention. Figure 7 shows only the peripheral area additionally iterated for illustrative purposes. The iterative procedure, of course, applies to the entire volume of the fractal distributor zone, to distribute exit or takeoff points across the volume occupied by a distributor 128 or 136. The number of additional iterations is limited only by manufacturing techniques.

The term "shallow", as used in this exhibition, is intended to distinguish beds contained in a conventional column. According to this invention, a bed 132 of a given volume is configured with a significantly reduced column height 144 (measured along the fluid flow path in the course, without considering orientation) and a correspondingly increased cross-sectional area ( measured transversely to the fluid flow path through the bed) compared to a conventional bed configuration. The use of the reader configuration allows the processing of a fluid through a bed 132 which has a height reduced by at least 70% compared to a given conventional fluid process. In fact, there are virtually no limits on bed height reduction, which can be obtained by practicing this invention. In contrast to most conventional resin beds, those according to this invention are characterized by significantly larger diameters; typically at least twice their heights. Diameter to height ratios of more than 10: 1 are practical, and ratios of more than 100: 1 are also currently considered practical. As an example, the embodiment illustrated in Figure 1 has a ratio of about 50: 1. .

Although other cross-sectional configurations are operable, a circular cross-sectional bed configuration is currently preferred. The term "diameter", as applied to other than circular configurations, should be understood to mean "effective diameter", that is, an intermediate dimension to the major and minor axes of any such configuration.

While other valuable benefits result from the use of stem cells in accordance with this invention, a particularly significant benefit is the reduction of certain process limiting characteristics. A useful benefit of this invention is the reduction of bandwidth and fluid overlap. The present invention does not require overpressed or compressed bed conditions. In fact, due to the fact that the invention does not require overpressure conditions, processes that require periodic or constant fluidization can be performed in the cell and still maintain the advantages of shallow bed operation. This reality greatly expands the possibilities for the use of the shallow bed concept. Nor does this invention require the particle-free cavities of U.S. Patent No. 5,626,750, and therefore will not exhibit the mixing effect which will occur in such chambers.

Moreover, one of the advancements provided by this invention is to avoid processing limitations, such as pressure loss across the taught bed in the '750.

Advantages of this invention:

1. Columns with very low bed depth and very high width to height ratio can be obtained.

2. An overpressured bed is not required to achieve uniform flow distribution through the apparatus.

3. Substantial pressure loss from the bed is not required to achieve a uniform flow distribution through the apparatus.

4. The flow to these devices can be significantly increased compared to a conventional cell design because of a large decrease in pressure loss across the bed.

5. The flow rate for these devices can be significantly increased because of a large decrease in linear velocity across the bed compared to an equivalent bed volume in a conventional high bed depth configuration.

6. The cost for the equipment is reduced because the same amount to be treated can be passed through a much smaller and therefore less expensive column.

7. Due to the fact that the equipment is smaller, there are simple savings in the space required for the disposal of the equipment.

8. The building materials parp? · - ^ uipaThento may be immersed e. therefore, less expensive because of the reduced structural requirements of this invention.

9. The invention creates possibilities for a cell construction using a wide range of normally unacceptable materials.

10. Costs for bed materials are reduced as much less is required for a given feed rate.

11. The reduced requirement for bed material allows a commonly expensive bed material to be used, thereby creating new opportunities previously negated due to the cost of bed material.

12. Due to the characteristics of reduced pressure loss, a highly compressible material can be used for the trim of the reader while maintaining high productivity.

13. Due to the reduced pressure loss characteristics, very small bed particles can be used and therefore have a faster reaction rate (high surface area per volume unit).

14. When used for cycling equipment, this invention allows these processes to complete cycles very quickly. One result is that peripheral equipment can be much shorter than usual, because equipment such as storage tanks does not have to store as much material.

15. The energy required for process operation is reduced for a given bed material, because of the reduction in bed pressure loss. For example, process pumps can be controlled with less engine power.

16. Overlap of fluid front is reduced. Examples of such benefits which can be obtained with this invention include a reduction in bandwidth which occurs in chromatography and a reduction in fluid overlap in other applications.

17. The use of shallow cells provides the benefits listed above when used in single or multiple cell configurations. Examples of multiple cell configurations for which this invention is beneficial are primary / secondary serial processing, etc., simulated moving bed processes and carousel-type fluid processing.

This invention allows the construction and operability of virtually unlimited fluid processing as to the "fineness" of the column bed. The advantages of very low bed pressure loss and reduced linear velocity across the bed are therefore realized. As noted earlier, there are virtually no limits on column height reduction, because a uniform fluid distribution can be recursively improved.

Although less demanding applications can operate sufficiently with a fractal density of less than 2,153 fluid outlets (or collection points) per square meter (200 fluid outlets (or takeoff points) per square foot) at the fluid / manifold interface to In a very fine distribution, a density of at least 310,000 fluid output (or collection points) per square meter (200 fluid outlets (or collection points) per square inch) is recommended. Much higher densities are in the contemplation, and it is recognized that a progressively higher density will allow progressively slower bed geometry and higher operating efficiency.

Example 1 - Pilot TestExample 1 - Pilot Test

This example describes a specific test, although this example is not intended to limit the scope of the invention. In fact, this particular application has been chosen because it clearly demonstrates in a single test many of the general benefits claimed above for shallow cell fluid processing with this invention. It should be clear that similar benefits will originate for different fluid applications.

For this test, an ion exchange application was evaluated. Ion exchange processes typically have a large proportion of the problems and limits listed above. A pilot cellular system was designed to soften the "fine juice" of a sugar beet factory. Such material is typically softened to best suit downstream processes. In this ion exchange process, the hardness of the dosuco (calcium and magnesium) is exchanged for monovalent constituents, including H + and / or Na + and / or K +.

A softening resin referred to as a weak cation exchange resin was used (Bayer CNP LF). The resin regenerator was sulfuric acid (hydrogen form regeneration) and the softening exhaust material was "fine juice" at approximately 15% DS, obtained from the processing of saccharine beets. The feed material and the re-generator are entirely conventional for soft cationic softening softening.

A shallow cell was constructed with a diameter of 60.96 cm (2ft). Fractal distributors were used as mirror images for both input distribution 128 and output collection 132. Flow was allowed in both downward and upward directions.

The bed depth of the weak cation ion exchange resin was 15.24cm (6 inches). The D: h ratio of the bed was 4: 1. To demonstrate that the shallow bed could be operated without the prior art requirement of an overpressured bed, 15.24 cm (6 inches) of void 156 above the 132 bed was included in the cell design (see Figure 3).

Exhaustion was a downward flow at 500 bed volumes per hour. This means that one juice volume was treated within one hour, equal to 500 volumes of the ion exchange resin bed. The operating temperature was 82 ° C. Regeneration was a downward flow with approximately 0.07 N H 2 SO 4 at 150 bed volumes per hour.

Softening was entirely satisfactory with the shallow cell compared to a conventional industrial system. The composite soft acid product was typically from 0 to 0.02 grams of CaO / 100 grams of dry substrate, which is in line with the requirements of the softened soft parasol industry. Commonly, a shallow deresine column would be expected to lose hardness due to turbulence and poor kinetics, particularly if the resin flow / unit was increased by a factor of 10. However, the shallow design of this invention allowed excellent results a10. times the conventional feed rate. The reason is that the apparatus maintained a completely homogeneous non-turbulent fluid flow. Also, the low bed depth reduced the linear flow rate, so the kinetics were still acceptable. If the same bed volume had been configured in the conventional vertical manner and the increased flow as in this test, the linear velocity would have been too high for an appropriate ion exchange kinetics. The fluid would have passed very quickly in front of the resin beads, thereby interfering with mass transfer. It was also noted that a conventional high bed at the high flow rates of this tester would result in extremely high pressure loss across the bed.

Following is a comparison of the state of the art of weak cation juice softening versus the shallow cell operation of this invention. Both systems were operated side by side in an industrial installation, so the comparison includes having an exactly comparable feed material. <table> table see original document page 18 </column> </row> <table>

Note that the shallow cell reduced the height of the required resin bed by 85%. This corresponds to the observation that the use of this invention generally reduces a given process bed depth by at least 70%.

Several benefits were observed in this pilot test. First, the flow through the shallow cell was 10 times higher compared to conventional equipment. It is noted that the literature refers to very high resin productivity systems, exactly in this application, providing a maximum of 50 bed volumes / hour of exhaust flow. However, with the shallow cell apparatus, the feed flow is increased by a order of magnitude.

Because productivity is increased by 10 times, the amount of resin required is reduced by 10 times. This means that the amount of resin is very small and the corresponding capital costs will be small. In this test, note the 85% reduction in deresin requirement. The very small amount of resin also means that the size of the equipment is reduced by about 10 times, thus resulting in lower equipment cost and the provision of valuable savings in equipment space requirements. Since the pressure through the bed was reduced by about 95% to 98%, it was possible to use a very low pressure vessel. This means that a low-cost thin-wall construction can be used, or if you have the option of using inexpensive, noncommonly suitable materials for pressure vessels, for example, low-cost plastics. Low bed pressure pressure also equals lower energy use required for fluid pumping.

Rapid but efficient cycling of the test suggests that much smaller peripheral equipment may be used, because storage tanks for a material such as regenerator and regeneration loss need to store only 1 / 10 of the conventional amount of material.

It is important to understand that if the bed volume in the pilot sample is increased in size to allow treatment of a larger amount of feed material, the very short depth of the piglet will remain or be further reduced. The additional bed volume is increased by increasing the column width. This is contrary to the usual scheduling methods, which would be based on increasing the volume of the bed by adding height to the bed.

Note that this example also demonstrated that an overpressured bed is not required for the operation of this invention. This is indicated by the fact that upward flow fluidization of the resin was possible (100% expansion) with no detrimental effects on subsequent regeneration or exhaustion steps.

Note, too, that this example demonstrated that loss of bed depression is not necessary to cause the required fluid distribution. In fact, the bed pressure loss was reduced to only 10.34 kPa (1.5 psi) compared to the conventional range of 344.74 to 551.58 kPa (50-80 psi). Therefore, the present apparatus operates at a reduced bed pressure loss by a factor of at least 30 compared to conventional devices. Even at a 34.47 kPa (5 psi) pressure loss across the bed, the present device reduces the loss in processing depression by at least one order of magnitude required by a conventional apparatus.

Example 2 - Construction Flexibility for Progressively Fine Scheduling

This invention can be applied across the full range of fluid processing scales, from very small scale applications to very large industrial use. The reason for this is that the fractional structures used in combination with the shallow cell / shallow bed design provide a continuous scaling function as the application scale changes.

Computer-aided machining, molding and conduit construction techniques are suitable for fractal construction. However, because this invention allows for a practically limitless and progressive reduction of the processing bed depth, the practical problem of how to fabricate a progressively finer scheduling structure may arise.

To demonstrate the practical application of this invention, a defractal type as in Figure 6 with a very small aspect size was constructed using stereolithography. The fractal was designed with a final output diameter of 0.381 mm (0.015 inch). For this shallow cell application, the fractal was designed as 10 plates. The plates were then manufactured as a monolithic part. Stereolithography is an aqual technique that allows for a very thin aspect size.

To further demonstrate that this invention is practically fabricated on very small scales which provide progressively wider and shallower bed depth, an identical fractal was fabricated using the photochemical etching technique. . This method introduces additional material options such as stainless steel and other metals.

It is noted that a particular manufacturing technique is not required for carrying out this invention, these examples only suggest the flexibility and immediate practicality of the construction. Laser fabrication techniques, micromachining, nanotechnology construction methods, ion deposition, etc. are appropriate, and it is recognized that future fabrication techniques for a small scale structure are likely to be suitable for obtaining the desired shallow depth of the appliance.

Applicability of this Invention to Multiple Cell Processes

Although the shallow cell apparatus of this invention may be used in single cell applications, a key purpose of this invention is to use such cells in multiple cell configurations. Multiple cell depth reduction processes will result in the same benefits of high productivity, cost savings, etc.

Examples of multiple cell configurations which will benefit from replacing conventional cells with shallow cells of this invention include:

1. A primary / secondary / serial type fluid processing / etc .. In these operations, the fluid flows out of a cell and then treated in a second and / or a third, etc.

2. Simulated moving bed technology. In this type of process, the fluid passes through 2 or more beds or specified sections of stationary material. Bed movement is typically simulated using its valve switching.

3. Carousel type systems. In this type of system, columns are mounted on a rotary table or a carousel, and rotate around a center guide shaft and a central distribution valve.

Note that these suggestions for multiple cell use are not intended to limit the applicability of the invention. This invention is generally useful as a substitute for conventional bed depth fluid processes. The present invention may be embodied in other specific forms without departing from its spirit or essential characteristics. The described modalities should be considered in all respects only as illustrative and not restrictive. The scope of the invention, therefore, is indicated by the appended claims rather than the foregoing description. Any changes which fall into the meaning and equivalence range of the claims should be involved in its scope.

Claims (14)

A fluid processing system comprising: a first resin bed (132) with an inlet end, an outlet end and a diameter equal to at least two times the distance between said inlet end and said outlet end: a first fluid dispenser (128) constructed and disposed to introduce fluid at said inlet end of the resin bed (132); a first fluid collector (136) disposed lower than said first resin bed to collect the once processed fluid at said outlet end of said processing bed; characterized in that: the first manifold (136) is arranged in a mirror image position relative to the first manifold (128), the first manifold (128) is constructed and arranged to collect the processed fluid once it exits the outlet end of the deresin bed (132); and the dispenser (128) and the resin bed (132) each define a continuous backwash and continuous operating void (156) of fluidized delight operation. System according to claim 1, characterized in that said manifold (136) is constructed and arranged to collect fluid through collection ports at a density of at least 2,153 square perimeter (200 per square foot). System according to claim 1, characterized in that said distributor (128) and said collector (136) are fractal. System according to claim 1, characterized in that the diameter to height ratio of said resin bed (132) is at least 10: 1. System according to Claim 1, characterized in that it is constructed and arranged for the production of process flow conditions with a pressure loss across said bed (132) of less than 34.47 kPa (5 psi). ). The system of claim 1 further comprising: a second resin bed (132) with an inlet side, an outlet side and a diameter equal to at least twice the distance between said one. inlet side and said outlet side, a second fluid distributor (128) constructed and arranged to introduce said once processed fluid into said inlet side of said second bed, said second distributor having a density of at least 2,153 distribution outputs per square meter (200 distribution outputs per square foot); and a second fluid collector (136) constructed and arranged to collect the processed fluid twice on said outlet side of said second resin bed (132). System according to claim 6, characterized in that each of said first and second fluid distributors (128) comprises a fractal structure. System according to claim 7, characterized in that each of said first and second fluid collectors (136) comprises a fractal structure. System according to claim 8, characterized by the fact that a recursive fractal element can be viewed as having an "H" format. A system according to claim 1, characterized in that said first fluid distributor (128) is constructed and arranged to introduce fluid into said resin soft inlet end (132) and includes a plurality of conduits (172). , each conduit (172) being divided into successive pluralities of conduit branches (174, 176) arranged in generations. System according to Claim 10, characterized in that each generation of conduit branches (174, 176) is arranged in a separate plane from the conduits of a respective prior generation and a respective subsequent generation of conduit branches. System according to claim 11, characterized in that each conduit branch has a distribution outlet. System according to claim 12, characterized in that said first fluid distributor (128) has a density greater than about 2,153 per square meter (200 per square pole). System according to claim 1, characterized in that said dispenser includes a plurality of outlets oriented in different directions from the fluid flow direction from the dispenser towards the resin bed.